A method for separating and refining 1-butene with a high purity and a high yield from a raffinate-2 stream. The method includes: feeding raffinate-2 to a first distillation column; obtaining heavy raffinate-3 from a lower part of the first distillation column; recovering an upper part fraction containing 1-butene from an upper part of the first distillation column; feeding the upper part fraction containing 1-butene to a second distillation column; recovering a first lower part fraction rich in 1-butene from a lower part of the second distillation column and light raffinate-3 from an upper part of the second distillation column. heat of the upper part fraction recovered from the upper part of the first distillation column is fed to the lower part of the second distillation column through a first heat exchanger. Thus, 1-butene is obtained with high purity and high yield while maximizing an energy recovery amount by double-effect distillation.
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1. A method of refining raffinate-2 comprising:
feeding a raffinate-2 containing n-butane, isobutane, and 1-butene to a first distillation column;
obtaining heavy raffinate-3 containing n-butane from a lower part of the first distillation column;
recovering an upper part fraction containing 1-butene from an upper part of the first distillation column;
feeding the upper part fraction containing 1-butene to a second distillation column; and
recovering a first lower part fraction rich in 1-butene recovered from a lower part of the second distillation column and a light raffinate-3 containing isobutane from an upper part of the second distillation column,
wherein heat of the upper part fraction recovered from the upper part of the first distillation column is fed to a second lower part fraction recovered from the lower part of the second distillation column through a first heat exchanger,
wherein the upper part fraction of the first distillation column is fed to the first heat exchanger to supply heat from the upper part of the first distillation column to the second lower part fraction through the first heat exchanger, a portion of the upper part fraction of the first distillation column passed through the first heat exchanger is fed as a middle feed stream to the second distillation column, and a remaining portion of the upper part fraction of the first distillation column passed through the first heat exchanger is refluxed as an upper feed stream to the upper part of the first distillation column,
wherein a position of the middle feed stream is lower than a position of the upper feed stream,
wherein an upper part pressure of the second distillation column is 4.7 kgf/cm2 or more, and
wherein an upper part pressure of the first distillation column is higher than the upper part pressure of the second distillation column by 3.5 kgf/cm2 to 5.5 kgf/cm2.
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3. The method of
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This application is the U.S. national stage of international Application No. PCT/KR2018/008223, filed Jul. 20, 2018, and claims priority from Korean Application No. 10-2017-0096789, filed Jul. 31, 2017, the contents of which are incorporated by reference as if fully set forth herein.
The present invention relates to a method of refining a raffinate-2 stream discharged from a process of separating a C4 mixture, and more specifically, to a method of separating and refining 1-butene with a high purity and a high yield from a raffinate-2 stream.
A C4-fraction from the naphtha cracking center (raw C4) is a mixture of C4 materials with a single bond, a double bond, or a triple bond, which is also referred to as a C4 mixture (mixed C4).
Generally, a subsequent process from the C4-fraction involves a process of separating and removing butadiene, which is a raw material for the synthetic rubber. The butadiene is separated and removed by, for example, extraction or extractive distillation. A C4 stream that remains after removing the butadiene is a hydrocarbon mixture (corresponding to raffinate-1 or hydrocracking-C4) containing saturated hydrocarbons (n-butane and isobutane) together with the olefin (isobutene, 1-butene, and 2-butene). A method of removing isobutene from the mixture is to react isobutene with methanol to form methyl tertiary butyl ether (MTBE). The C4 mixture obtained after removing the butadiene and isobutene is referred to as raffinate-2 (see
Components of the C4 mixture have small differences in boiling points and low separating factors, and thus it is difficult and uneconomical to perform distillation subsequent treatment that separates desired components in each step. In particular, it is not easy to separate 1-butene, which is separated from the raffinate-2, from a refinement process since 1-butene has almost the same boiling point as isobutene. The boiling point of isobutene is −6.9□ and the boiling point of 1-butene is −6.24□. In particular, when a ratio of isobutene/1-butene in a feed is high, it is difficult to design the refinement process, and in severe cases, there is a problem in that it is not possible to manufacture products. Therefore, it is necessary to develop a process capable of efficiently separating 1-butene with a high purity from the raffinate-2.
An object of the present invention is to provide an energy-saving process capable of recovering 1-butene with a high purity and a high yield from a raffinate-2 stream.
In one general aspect, a method of refining raffinate-2 includes:
feeding a raffinate-2 containing n-butane, isobutane and 1-butene to a first distillation column to obtain heavy raffinate-3 containing n-butane from a lower part of the first distillation column and to recover an upper part fraction containing 1-butene from an upper part of the first distillation column; and
feeding the upper part fraction containing 1-butene to a second distillation column to recover a first lower part fraction rich in 1-butene from a lower part of the second distillation column and to recover light raffinate-3 containing isobutane from an upper part of the second distillation column,
wherein heat of the upper part fraction recovered from the upper part of the first distillation column is fed to the lower part of the second distillation column through a first heat exchanger.
The raffinate-2 fed to the first distillation column may contain isobutene and 1-butene at a weight ratio (isobutene/1-butene) of 0.006 or less.
An operating pressure of the second distillation column may be 4.7 kgf/cm2 or more.
An operating pressure of the first distillation column may be higher than an operating pressure of the second distillation column by 3.5 kgf/cm2 or more.
The upper part fraction of the first distillation column may be fed with heat to a second lower part fraction recovered from the lower part of the second distillation column through the first heat exchanger, a portion of the upper part fraction of the first distillation column may be fed with a feed stream to the second distillation column, and the remainder may be refluxed to the upper part of the first distillation column.
The second lower part fraction of the second distillation column that is fed with heat through the first heat exchanger may be refluxed to the second distillation column.
A portion of the first lower part fraction of the second distillation column may be reheated and then refluxed.
All of the upper part fraction of the first distillation column may be fed to the first heat exchanger, and a separate condenser may not be provided in the upper part of the first distillation column.
The heavy raffinate-3 recovered from the lower part of the first distillation column may be reheated, used to preheat the raffinate-2 fed to the first distillation column through a second heat exchanger, and then recovered.
A portion of the heavy raffinate-3 that is reheated after being recovered from the lower part of the first distillation column may be refluxed.
According to the present invention, 1-butene having a purity of 99.0% or more is capable of being recovered at a yield of 80% or more while maximizing heat quantity recovered in a heat exchanger in a process of refining the raffinate-2 stream to reduce energy by 30% or more.
Hereinafter, a method according to the present invention is described with reference to
The present invention relates to a method for economically separating and refining 1-butene with a high purity and a high yield from a raffinate-2 stream discharged from a separation process of a C4 mixture.
In the method according to the invention, raffinate-2 may be all commercially available C4 hydrocarbon mixtures having 1-butene, n-butane, and isobutene. Suitable isobutene-based C4 streams, may be, for example, those obtained in a post-treatment of the stream, such as, those obtained by a refiner, a cracker (e.g. a steam cracker, a cat cracker), Fischer-Tropsch synthesis, dehydrogenation of butane, skeleton isomerization of linear butene, and metathesis of olefins.
The method of refining raffinate-2 according to the present invention includes:
feeding a raffinate-2 10 containing n-butane, isobutane, and 1-butene to a first distillation column C1 to obtain heavy raffinate-3 13 containing n-butane from a lower part of the first distillation column C1 and to recover an upper part fraction 12 containing 1-butene from an upper part of the first distillation column; and
feeding the upper part fraction 12 containing 1-butene to a second distillation column C2 to recover a first lower part fraction 21 rich in 1-butene from a lower part of the second distillation column C2 and to recover light raffinate-3 22 containing isobutane from an upper part of the second distillation column,
wherein heat of the upper part fraction 12 recovered from the upper part of the first distillation column C1 is fed to the lower part of the second distillation column C2 through a first heat exchanger E1.
Here, the raffinate-2 10 fed to the first distillation column C1 preferably contains isobutene and 1-butene at a weight ratio (isobutene/1-butene) of 0.006 or less. This is because 1-butene is not easily separated in a refinement process since 1-butene has almost the same boiling point as isobutene (the boiling point of isobutene is −6.9□ and the boiling point of 1-butene is −6.24□) and it was found that when the ratio of isobutene/1-butene in a feed is higher than 0.0006, it is difficult to design the refinement process, and in severe cases, there is a problem in that it is not possible to manufacture products.
Further, an operating pressure of the second distillation column C2 is preferably 4.7 kgf/cm2 or more, and an operating pressure of the first distillation column is preferably higher than an operating pressure of the second distillation column by 3.5 kgf/cm2 or more. This is because it was found that a condensation temperature of the first distillation column is advantageous for double-effect distillation (DEC) which allows to have pressure sufficient to heat the second distillation column. The preferred range thereof is 3.5 to 5.5 kgf/cm2, or 3.5 to 5.0 kgf/cm2, or 4.0 to 5.5 kgf/cm2 or 4.0 to 5.0 kgf/cm2.
The upper part fraction 12 of the first distillation column C1 may be fed with heat to the second lower part fraction 23 recovered from the lower part of the second distillation column C2 through the first heat exchanger E1, a portion 12-1 of the upper part fraction of the first distillation column may be fed with a feed stream to the second distillation column C2, and the remainder 12-2 may be refluxed to the upper part of the first distillation column C1.
Further, the second lower part fraction 23 of the second distillation column C2 that is fed with heat through the first heat exchanger E1 is refluxed to the second distillation column C2.
Further, a portion 25 of the first lower part fraction 21 of the second distillation column C2 may be reheated and then refluxed to the second distillation column C2.
It is advantageous to divide the lower part fraction of the second distillation column C2 into the first lower part fraction 21 and the second lower part fraction 23 and inject each divided fraction into the heat exchanger since it is usable when all of the heat quantities required for start-up for an initial process and the second distillation column in a reheater b2 are not capable of being fed.
According to an embodiment, all of the upper part fraction 12 of the first distillation column C1 may be fed to the first heat exchanger E1, and a separate condenser may not be provided in the upper part of the first distillation column C1. In other words, the condenser may be omitted by double-effect distillation (DEC) using the first heat exchanger.
The heavy raffinate-3 11 recovered from the lower part of the first distillation column C1 may be reheated, used to preheat the raffinate-2 10 fed to the first distillation column C1 through a second heat exchanger E2, and then recovered.
Here, a portion 15 of the heavy raffinate-3 that is reheated after being recovered from the lower part of the first distillation column C1 may be refluxed.
The method according to the present invention has recovered heat quantity of 6 Gcal/hr or more, thus resulting in very good energy saving effect.
Hereinafter, Examples of the present invention are described.
Refinement was performed using raffinate-2 having properties described in Table 1 below and employing the process illustrated in
TABLE 1
Component
Mass Frac.
C3's
0.48%
C4 paraffin
29.18%
Butene-1
43.73%
Isobutene
0.25%
C4 olefin
25.94%
C5's
0.42%
Sum
100.00%
Refinement of raffinate-2 was performed in the same manner as in Example 1, except that preheating (E2) of raffinate-2 was performed as illustrated in
Refinement of raffinate-2 was performed in the same manner as in Example 2, except that a difference in operating pressure between the heavy end elimination column C1 and the light end elimination column C2 was 5.5 kgf/cm2.
The refinement process was performed by using the same raffinate-2 as in Example 1, but not applying double-effect distillation as shown in
The refinement process was performed in the same manner as in Example 1, except that a ratio of isobutene/1-butene in raffinate-2 was 1% and a difference in operating pressure between the heavy end elimination column C1 and the light end elimination column C2 was 1.1 kgf/cm2.
The refinement process was performed in the same manner as in Comparative Example 2, except that a ratio of isobutene/1-butene in raffinate-2 was 0.6% and the operating pressure of the light end elimination column C2 was reduced to 4 kgf/cm2.
The refinement process was performed in the same manner as in Comparative Example 2, except that a ratio of isobutene/1-butene in raffinate-2 was 0.6% and a difference in operating pressure between the heavy end elimination column C1 and the light end elimination column C2 was 2.1 kgf/cm2.
Table 2 shows comparison results of specific operating conditions and energy recovery rates of Examples 1 to 3 and Comparative Examples 1 to 4.
TABLE 2
Comparative
Comparative
Comparative
Comparative
Example 1
Example 2
Example 3
Example 4
Example 1
Example 2
Example 3
Feed
Iso-butene/
0.6
1.0
0.6
0.6
0.6
0.6
0.6
Condition
Butene-1 (%)
Heavy
Upper Part
5.7
5.7
5.7
8.7
10.1
10.1
12.1
End Cut
Pressure
Column
(kgf/cm2)
Upper Part
51.8
51.8
51.8
67.1
73.1
73.1
80.8
Temperature
(□)
Feed
40.0
40.0
40.0
40.0
40.0
60.7
40.0
Temperature
(□)
Cond. Q
5.27
5.27
5.27
6.07
6.51
6.55
7.25
(Gcal/hr)
Reb. Q
5.40
5.40
5.40
6.30
6.78
6.69
7.58
(Gcal/hr)
Light
Upper Part
6.6
6.6
4.0
6.6
6.6
6.6
6.6
End Cut
Pressure
Column
(kgf/cm2)
Upper Part
51.3
51.3
35.3
51.3
51.3
51.3
51.3
Temperature
(□)
Lower Part
61.9
61.9
46.8
61.9
61.9
61.9
61.9
Temperature
(□)
Product
Spec.
Spec.
Spec.
Spec.
Spec.
Spec.
Spec.
Purity (%)
in
Out
in
in
in
in
in
Cond. Q
5.92
5.92
3.84
6.40
6.72
6.71
7.52
(Gcal/hr)
Reb. Q
5.94
5.94
3.81
6.37
6.68
6.67
7.45
(Gcal/hr)
Energy
Process-
0.00
0.00
0.00
0.00
6.51
6.55
7.25
Comparison
recovered
Heat
(Gcal/hr)
Heat Used
11.21
11.21
5.27
12.44
6.72
6.71
7.52
for CW
(Gcal/hr)
Heat Used for
0.00
0.00
3.84
0.00
0.00
0.00
0.00
Refrigerant
(Gcal/hr)
Total Q
11.34
11.34
9.21
12.67
6.95
6.81
7.78
(Gcal/hr)
Saving Rate
—
0.00
18.78
−11.73
38.71
39.95
31.39
(%)
It could be appreciated from the above-described results that when the weight ratio of isobutene/1-butene in the raffinate-2 to be fed was more than 0.006 (0.6%), it was not possible to satisfy the product specification (99.9% or more) (Comparative Example 2), and when the operating pressure of the light end elimination column (C2) was reduced, thus resulting in an increase of the refrigerant cost and an increase in the energy cost (Comparative Example 3).
In addition, it could be appreciated that when the difference in pressure of the upper part between the heavy end elimination column C1 and the light end elimination column C2 was less than 3.5 kgf/cm2, it was not possible to achieve heat exchange according to double-effect distillation (Comparative Example 4).
On the other hand, it could be appreciated that in Examples 1 to 3 that the difference in pressure of the upper part between the heavy end elimination column C1 and the light end elimination column C2 was 3.5 kgf/cm2 or more, and thus the heat exchange was achieved, and 6 Gcal/hr of heat could be recovered, thereby obtaining an energy saving rate of 30% or more. In addition, it could be appreciated that when the pressure difference was 5.5 kgf/cm2, the energy saving rate was slightly reduced, and thus the optimum pressure difference was in the range of 3.5 to 5.5 kgf/cm2.
Although the present invention has been described with reference to preferred embodiments thereof, the scope of the present invention is not limited thereto, and specific portions of the contents of the present invention have been described in detail. Thus, it will be apparent to those skilled in the art that these specific descriptions are merely preferred embodiments and that the scope of the invention is not limited thereto. Therefore, the substantial scope of the present invention is defined by the accompanying claims and equivalents thereof.
Lee, Sung Kyu, Shin, Joon Ho, Kim, Sung Kyun, Kim, Ji Hye, Beyun, Yong Mann
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